CN105505412A - Moving bed pyrolysis reactor - Google Patents
Moving bed pyrolysis reactor Download PDFInfo
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- CN105505412A CN105505412A CN201610055231.1A CN201610055231A CN105505412A CN 105505412 A CN105505412 A CN 105505412A CN 201610055231 A CN201610055231 A CN 201610055231A CN 105505412 A CN105505412 A CN 105505412A
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- 238000000197 pyrolysis Methods 0.000 title claims abstract description 64
- 239000000463 material Substances 0.000 claims abstract description 36
- 238000003756 stirring Methods 0.000 claims abstract description 26
- 238000009825 accumulation Methods 0.000 claims description 58
- 238000009795 derivation Methods 0.000 claims description 14
- 230000001172 regenerating effect Effects 0.000 abstract description 4
- 238000005336 cracking Methods 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 84
- 239000003921 oil Substances 0.000 description 49
- 238000000034 method Methods 0.000 description 17
- 239000010410 layer Substances 0.000 description 15
- 239000003245 coal Substances 0.000 description 13
- 230000008569 process Effects 0.000 description 13
- 239000000567 combustion gas Substances 0.000 description 9
- 230000004888 barrier function Effects 0.000 description 8
- 230000008901 benefit Effects 0.000 description 7
- 239000004215 Carbon black (E152) Substances 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- 229930195733 hydrocarbon Natural products 0.000 description 6
- 150000002430 hydrocarbons Chemical class 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 5
- 230000001276 controlling effect Effects 0.000 description 5
- 239000007787 solid Substances 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- 238000012546 transfer Methods 0.000 description 5
- 238000004939 coking Methods 0.000 description 4
- 239000003077 lignite Substances 0.000 description 4
- 238000004458 analytical method Methods 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 238000001035 drying Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- 239000000446 fuel Substances 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 230000005855 radiation Effects 0.000 description 3
- 230000001105 regulatory effect Effects 0.000 description 3
- 241000209094 Oryza Species 0.000 description 2
- 235000007164 Oryza sativa Nutrition 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 238000002309 gasification Methods 0.000 description 2
- 239000010903 husk Substances 0.000 description 2
- 230000008676 import Effects 0.000 description 2
- 230000035800 maturation Effects 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 235000009566 rice Nutrition 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 239000000969 carrier Substances 0.000 description 1
- 239000012159 carrier gas Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000012512 characterization method Methods 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 238000005338 heat storage Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 239000011229 interlayer Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000011020 pilot scale process Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- -1 resinous shale Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
- C10B47/18—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge
- C10B47/20—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge according to the moving bed type
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
- C10B47/28—Other processes
- C10B47/32—Other processes in ovens with mechanical conveying means
- C10B47/44—Other processes in ovens with mechanical conveying means with conveyor-screws
Abstract
The invention discloses a moving bed pyrolysis reactor. The moving bed pyrolysis reactor comprises a material inlet, a semicoke outlet, regenerative radiant tubes, oil gas outlet pipelines, a stirring device and a gas collecting tube, wherein the material inlet is located in the top of the reactor, and the semicoke outlet is located in the bottom of the reactor; the multiple layers of regenerative radiant tubes are arranged inside the reactor in the height direction of the reactor, and the regenerative radiant tubes on each layer are parallel in the horizontal direction; through holes are formed in the wall of each oil gas outlet pipeline; the stirring device comprises a stirring shaft and a plurality of stirring rods connected to the stirring shaft, and the stirring shaft stretches into the reactor through the semicoke outlet and can rotate in the reactor; the gas collecting tube comprises a collecting main and branch gas collecting tubes communicated with the collecting main, the collecting main is vertically arranged outside the reactor, and the branch gas collecting tubes penetrate through the side wall of the reactor and stretch into the reactor to be communicated with the oil gas outlet pipelines. By the adoption of the reactor, secondary cracking of oil gas can be effectively restrained, and the yield of pyrolysis tar is increased.
Description
Technical field
The invention belongs to chemical field, specifically, the present invention relates to a kind of moving bed pyrolysis reactor.
Background technology
The energy structure present situation of China is rich coal, oil-poor, weak breath, and world today's hydrocarbon resources reduces gradually, day by day deficient, and China's hydrocarbon resources shortage is particularly serious, a large amount of hydrocarbon resources dependence on import.Hydrocarbon resources scarcity seriously governs China's economy and social development, and the burning of a large amount of fossil oil, brings again serious environmental problem simultaneously, as dust, and PM2.5, acid rain, greenhouse gases etc.Open up coal liquifaction, gas maked coal technology, pyrolysis, gasification, liquefaction technology etc. energetically, effectively can alleviate China's hydrocarbon resources shortage on the one hand, the poverty-stricken situation of heavy dependence import; Reduce the utilization of the fossil oils such as coal on the other hand, can effectively solve, at present, the environmental problem that China's rapid economic development faces.According to incompletely statistics, there are the brown coal of more than 90% in China for station boiler and various Industrial Boiler.The low-rank coal such as brown coal are directly burnt as power fuel, not only waste the hydrocarbon rich resource contained in coal, and efficiency is low, it is heavy to pollute.By middle low temperature pyrogenation technology and coal-char combustion, decoupling zero of gasifying, realizing low-rank coal classification high-efficiency cleaning trans-utilization, is the Main way of present large-scale Coal Chemical Industry.Meanwhile, for the IGCC technology of China's high-sulfur, high ash, very large economical efficiency, social benefit and environmental benefit can be realized.
Modern Coal-based Chemical is the high-efficiency cleaning trans-utilization realizing the carbonaceous fuels such as low-rank coal, develop multiple comprehensive coal chemical technology, pyrolysis-burning decoupling zero, pyrolysis-chemical decoupling zero, pyrolysis-gasification decoupling zero etc., but really realize industrialized few, the process of amplifying from pilot scale to industrialization, encounter various technical barrier.Wherein especially with pyrolysis reactor design, subsequent purification treatment process is particularly outstanding.At present, the main type of furnace of carbonaceous fuel (coal, resinous shale, biomass etc.) pyrolysis has the solid heat carrier retort of Fushun stove, three river side's stoves, Dalian University of Science & Engineering, loves the Galoter stove of husky Leah and the ATP stove of Australia etc.Some gas retorts can only be used for the block resinous shale of pyrolysis and coal, and small particle size material cannot utilize, and resource utilization is low, and pulverulent material is because utilizing and bulk deposition; Take gas as the type of furnace of thermal barrier, because condensate recovery system is huge, the problems such as pyrolysis gas calorific value is low, and tar yield is low, are difficult to further genralrlization demonstration; Take solid as the type of furnace of thermal barrier, then there is raw material and thermal barrier Homogeneous phase mixing, the problems such as separation, and limit it and further develop.
Therefore, existing pyrolytic technique is further improved.
Summary of the invention
The present invention is intended to solve one of technical problem in correlation technique at least to a certain extent.For this reason, one object of the present invention is to propose a kind of moving bed pyrolysis reactor, this reactor effectively can suppress the second pyrolysis of oil gas, improve pyrolytic tar productive rate, and have employed heat accumulating type without thermal barrier heat accumulation type radiant tube heating technique, without the need to gas, solid thermal barrier, improve the calorific value of pyrolysis gas, simultaneously to have taken into account equipment few, easy to operate for moving bed pyrolysis reactor, the advantages such as failure rate is low.
In one aspect of the invention, the present invention proposes a kind of moving bed pyrolysis reactor, according to embodiments of the invention, this reactor comprises:
Material inlet and semicoke outlet;
Described material inlet is positioned at the top of described reactor;
Described semicoke outlet is positioned at the bottom of described reactor;
Heat accumulation type radiant tube, the short transverse multilayer of described heat accumulation type radiant tube in the inside of described moving bed pyrolysis reactor along described reactor is arranged, every layer has many heat accumulation type radiant tubes parallel to each other in the horizontal direction;
Oil gas derives pipeline, and the tube wall of described oil gas derivation pipeline is provided with through hole;
Whipping appts, described whipping appts comprises stir shaft and is connected to the multiple agitator arms on described stir shaft, and described stir shaft is extend into the inside of described reactor by described semicoke outlet and is configured to rotate in described reactor;
Effuser, the gas-collecting branch pipe that described effuser comprises gas gathering manifold and is connected with described gas gathering manifold,
Wherein, it is outside that described gas gathering manifold is arranged on described reactor vertically,
The sidewall that described gas-collecting branch pipe extends through described reactor to extend in described reactor and derives pipeline with described oil gas and is connected.
Thus, the second pyrolysis of oil gas effectively can be suppressed according to the moving bed pyrolysis reactor of the embodiment of the present invention, improve pyrolytic tar productive rate, and have employed heat accumulating type without thermal barrier heat accumulation type radiant tube heating technique, without the need to gas, solid thermal barrier, improve the calorific value of pyrolysis gas, simultaneously to have taken into account equipment few, easy to operate for moving bed pyrolysis reactor, the advantages such as failure rate is low, additionally by pyrolysis reactor, whipping appts is set, can enhancement of heat transfer effect.
In some embodiments of the invention, described gas-collecting branch pipe is multiple, and arranged parallel to each other along the length direction of described gas gathering manifold.Thus, the oil gas that can significantly improve in reactor derives efficiency.
In some embodiments of the invention, described gas-collecting branch pipe is perpendicular to described gas collecting main pipe.
In some embodiments of the invention, described oil gas is derived pipeline and is arranged along the short transverse multilayer of described reactor, and every layer has many oil gas derivation pipelines parallel to each other in the horizontal direction.Thus, the oil gas that can improve further in reactor derives efficiency.
In some embodiments of the invention, described oil gas derives pipeline and described heat accumulation type radiant tube is arranged in parallel, and the described heat accumulation type radiant tube left and right sides is separately symmetrically arranged with two oil gas derivation pipelines.Thus, the oil gas that can improve further in reactor derives efficiency.
In some embodiments of the invention, described oil gas derives pipeline with the spacing of the tube wall of contiguous described heat accumulation type radiant tube is that described oil gas derives the 1/2-3 of pipe diameter d doubly.In some embodiments of the invention, the tube wall that described oil gas derives pipeline is provided with multiple through hole.Thus, the oil gas that can improve further in reactor derives efficiency.
In some embodiments of the invention, described through hole is uniformly distributed on the length direction of described oil gas derivation pipeline.In some embodiments of the invention, oil gas described in same layer is derived pipeline and is communicated to same described gas-collecting branch pipe.
In some embodiments of the invention, all there is one or more agitator arm the top of every layer of radiator tube, and the vertical range of agitator arm and radiator tube is 20 ~ 300mm.Thereby, it is possible to enhancement of heat transfer effect.Such as, agitator arm can between radiation tube layer and oil gas delivery line channel layer for pyrolytic tar.
In some embodiments of the invention, described agitator arm is perpendicular to described stir shaft, and spaced apart along the length direction of described stir shaft.Thus, the yield of pyrolytic tar can be improved further.
In some embodiments of the invention, the adjacent projections of described agitator arm on the same cross section of described stir shaft at an angle.Thus, the yield of pyrolytic tar can be improved further.
In some embodiments of the invention, the angle ranging from 0 ~ 90 degree, not containing end value, preferably, the angle ranging from 30 ~ 90 degree, not containing 90 degree.Thus, the yield of pyrolytic tar can be improved further.
Additional aspect of the present invention and advantage will part provide in the following description, and part will become obvious from the following description, or be recognized by practice of the present invention.
Accompanying drawing explanation
Above-mentioned and/or additional aspect of the present invention and advantage will become obvious and easy understand from accompanying drawing below combining to the description of embodiment, wherein:
Fig. 1 is the structural representation of moving bed pyrolysis reactor according to an embodiment of the invention;
Fig. 2 is the vertical view of the whipping appts according to an embodiment of the invention on moving bed pyrolysis reactor;
Fig. 3 is the structural representation of the moving bed pyrolysis reactor according to another embodiment of the present invention.
Embodiment
Be described below in detail embodiments of the invention, the example of described embodiment is shown in the drawings, and wherein same or similar label represents same or similar element or has element that is identical or similar functions from start to finish.Be exemplary below by the embodiment be described with reference to the drawings, be intended to for explaining the present invention, and can not limitation of the present invention be interpreted as.
In describing the invention, it will be appreciated that, term " " center ", " longitudinal direction ", " transverse direction ", " length ", " width ", " thickness ", " on ", D score, " front ", " afterwards ", " left side ", " right side ", " vertically ", " level ", " top ", " end ", " interior ", " outward ", " clockwise ", " counterclockwise ", " axis ", " radial direction ", orientation or the position relationship of the instruction such as " circumference " are based on orientation shown in the drawings or position relationship, only the present invention for convenience of description and simplified characterization, instead of indicate or imply that the device of indication or element must have specific orientation, with specific azimuth configuration and operation, therefore limitation of the present invention can not be interpreted as.
In the present invention, unless otherwise clearly defined and limited, the term such as term " installation ", " being connected ", " connection ", " fixing " should be interpreted broadly, and such as, can be fixedly connected with, also can be removably connect, or integral; Can be mechanical connection, also can be electrical connection; Can be directly be connected, also indirectly can be connected by intermediary, can be the connection of two element internals or the interaction relationship of two elements, unless otherwise clear and definite restriction.For the ordinary skill in the art, above-mentioned term concrete meaning in the present invention can be understood as the case may be.
In the present invention, unless otherwise clearly defined and limited, fisrt feature second feature " on " or D score can be that the first and second features directly contact, or the first and second features are by intermediary indirect contact.And, fisrt feature second feature " on ", " top " and " above " but fisrt feature directly over second feature or oblique upper, or only represent that fisrt feature level height is higher than second feature.Fisrt feature second feature " under ", " below " and " below " can be fisrt feature immediately below second feature or tiltedly below, or only represent that fisrt feature level height is less than second feature.
In one aspect of the invention, the present invention proposes a kind of moving bed pyrolysis reactor.Moving bed pyrolysis reactor below with reference to Fig. 1-3 pairs of embodiment of the present invention is described in detail.According to embodiments of the invention, moving bed pyrolysis reactor comprises: material inlet 101, heat accumulation type radiant tube 11, oil gas derive pipeline 12, semicoke outlet 102, whipping appts 13 and effuser 14.
According to embodiments of the invention, material inlet 101 is positioned at the top of reactor, and is suitable for material to be supplied in reactor.
According to embodiments of the invention, semicoke outlet 102 can be arranged on the bottom of reactor, and is suitable for pyrogenous origin semicoke to discharge reactor.
According to embodiments of the invention, heat accumulation type radiant tube 11 is arranged along the short transverse multilayer of reactor in the inside of moving bed pyrolysis reactor, every layer has many heat accumulation type radiant tubes parallel to each other in the horizontal direction, according to a particular embodiment of the invention, heat accumulation type radiant tube parallel to each other is in the horizontal direction uniformly distributed, preferably, the heat accumulation type radiant tube arranged along the short transverse of reactor is parallel to each other and be staggeredly arranged.According to concrete example of the present invention, the caliber of heat accumulation type radiant tube can be 100 ~ 300mm.According to embodiments of the invention, the horizontal throw between adjacent heat accumulation type radiant tube outer wall is 200 ~ 500mm, and the vertical distance between adjacent heat accumulation type radiant tube outer wall is 200 ~ 700mm.It should be explained that, horizontal throw between adjacent heat accumulation type radiant tube outer wall can be understood as the distance on same layer between heat accumulation type radiant tube outer wall, and the vertical distance between adjacent heat accumulation type radiant tube outer wall can be understood as adjacent upper and lower two interlayers adjacent heat accumulation type radiant tube outer wall between distance.
According to embodiments of the invention, the number of plies of multilayer heat accumulation type radiant tube can be 10-25 layer.Contriver finds, this kind of structural arrangement can make reactor temperature field distribution even, thus can significantly improve the pyrolysis efficiency of material.
According to embodiments of the invention, heat accumulation type radiant tube can be unidirectional regenerative gas heat accumulation type radiant tube, and the heat namely produced by combustion gas by heat accumulation type radiant tube body carries out heat supply in the mode of radiation.According to a particular embodiment of the invention, heat accumulation type radiant tube can be provided with gas control valve (not shown).Thus, the flow passing into the combustion gas of heat accumulation type radiant tube can be regulated to wait the accurate temperature controlling realized pyrolytic process by adjustment gas control valve, thus the pyrolysis efficiency of material can be significantly improved, and then improve the yield of pyrolytic tar.
Concrete, the accurate temperature controlling of the realizations such as the flow of the combustion gas of heat accumulation type radiant tube to pyrolytic process can be passed into by adjustment, and heat accumulation type radiant tube adopts the combustion system of regularly commutation, the temperature field of single heat accumulation type radiant tube is made to be more or less the same in 30 DEG C, thus ensure the homogeneity of reactor temperature field, such as the adjustment temperature range of the heat accumulation type radiant tube in epimere region in reactor is made to be 500 ~ 800 DEG C by adjusting the flow passing into the combustion gas of heat accumulation type radiant tube, ensure the abundant pyrolysis of material, the flow being passed into the combustion gas of heat accumulation type radiant tube by adjustment makes the adjustment temperature range of the heat accumulation type radiant tube in hypomere region in reactor be 450 ~ 650 DEG C, thus a heating part does not further have the material of complete pyrolysis.
According to embodiments of the invention, the tube wall of oil gas derivation pipeline 12 is provided with through hole, according to a particular embodiment of the invention, oil gas is derived pipeline 12 and is arranged along the short transverse multilayer of reactor, and every layer has many oil gas derivation pipelines parallel to each other in the horizontal direction.
According to a particular embodiment of the invention, oil gas is derived pipeline 12 and is arranged in parallel with heat accumulation type radiant tube 11, and the left and right sides of heat accumulation type radiant tube 11 is symmetrically arranged with two oil gas derivation pipelines 12.Contriver finds, derive pipeline by installing oil gas in every root heat accumulation type radiant tube both sides, the oil gas that pyrolysis produces is derived pipeline by oil gas and is derived rapidly, thus restrained effectively the second pyrolysis of oil gas, and then improve the yield of pyrolytic tar, good in economic efficiency.According to concrete example of the present invention, the caliber that oil gas derives pipeline can be 30 ~ 80mm.，
According to a particular embodiment of the invention, oil gas derives pipeline with the spacing of the tube wall of contiguous heat accumulation type radiant tube is that oil gas derives the 1/2-3 of pipe diameter d doubly.The pyrolytic tar of generation can be derived thus at once, avoid pyrolytic tar cracking, improve pyrolytic tar productive rate.
According to a particular embodiment of the invention, the tube wall of oil gas derivation pipeline 12 is provided with multiple through hole, preferably, multiple through hole is derived on the length direction of pipeline 12 at oil gas and is uniformly distributed.Thus can so that pyrolytic tar be derived fast.
According to embodiments of the invention, multiple agitator arms 16 that whipping appts 13 comprises stir shaft 15 and is connected on stir shaft 15, thus stir shaft 15 drives agitator arm 16 to rotate under the driving of drive-motor, according to a particular embodiment of the invention, stir shaft 15 rotatably extend into inside reactor from semicoke outlet 102.Invention finds, by arranging whipping appts in reactor, agitator arm, in the process carrying out back rotation, effectively can avoid the coking on radiator tube surface, and then avoids reducing heat transfer efficiency because of radiator tube coking, thus can enhance heat transfer effect.
According to a particular embodiment of the invention, all there is one or more agitator arm the top of every layer of radiator tube, and the vertical range of agitator arm and radiator tube is 20 ~ 300mm.Can avoid the upper coking of radiator tube thus, guarantee equipment normally runs.Such as, agitator arm can between radiation tube layer and oil gas delivery line channel layer.
According to a particular embodiment of the invention, agitator arm 16 is perpendicular to stir shaft 15, and spaced apart along the length direction of stir shaft 15.
According to a particular embodiment of the invention, the adjacent projections of agitator arm 16 on the same cross section of stir shaft 15 at an angle.Such as, as shown in Figure 2, described angle θ can be 0 ~ 90 degree (not containing end value), preferably 30 ~ 90 degree (not containing 90 degree).Thus, agitator arm can be made effectively to loosen inside reactor material, thus oil gas pyrolytic tar can be derived fast.The length of central stirring shaft can be 1-18m, and detachable agitator arm vertical spacing can be 0.4-1m, and the number of plies can be 11-26 layer.
According to embodiments of the invention, the gas-collecting branch pipe 18 that effuser 14 comprises gas gathering manifold 17 and is communicated with gas gathering manifold 17, according to a particular embodiment of the invention, gas gathering manifold 17 is arranged on reactor outside vertically, and the sidewall that gas-collecting branch pipe 18 extends through reactor to extend in reactor and derives pipeline 12 with oil gas and is connected.Thus, enter oil gas derivation pipeline pyrolytic tar gas and be collected to gas gathering manifold through gas-collecting branch pipe.
According to a particular embodiment of the invention, gas-collecting branch pipe 18 is multiple, and multiple gas-collecting branch pipe 18 can be arranged parallel to each other along the length direction of gas gathering manifold 17, and according to concrete example of the present invention, gas-collecting branch pipe 18 is perpendicular to gas collecting main pipe 17.Thus, multiple gas-collecting branch pipe can ensure that oil gas derives the quick derivation of pyrolytic tar gas in pipeline, thus significantly improves the yield of pyrolytic tar.
According to concrete example of the present invention, as shown in Figure 1, same layer oil gas is derived pipeline 12 and is communicated to same gas-collecting branch pipe 18.
According to embodiments of the invention, reactor head can spherically type or taper.
According to embodiments of the invention, the bottom of reactor can be back taper.Thus, pyrogenous origin semicoke can be made to discharge reactor smoothly.
Thermal source is provided by using many group heat accumulation type radiant tubes for pyrolytic process according to the moving bed pyrolysis reactor of the embodiment of the present invention, the flow that can pass into the combustion gas of heat accumulation type radiant tube by adjustment realizes the accurate temperature controlling to pyrolytic process, and heat accumulation type radiant tube passes through heat storage type combustion, ensure that the homogeneity in temperature field, thus the pyrolysis efficiency of material can be significantly improved, and then improve the yield of pyrolytic tar, more traditional use gaseous heat-carrier or solid thermal carriers are compared as the pyrolytic reaction device of pyrolysis thermal source simultaneously, moving bed pyrolysis reactor of the present invention does not need to arrange preheating unit and carrier separating unit, thus can greatly simplify pyrolytic reaction technical process, and then significantly reduce device failure rate and in gained pyrolytic tar dust content lower, and funnel temperature is low, secondly the present invention is by arranging that in the both sides of heat accumulation type radiant tube oil gas derives pipeline, the oil gas that pyrolysis produces can be derived rapidly, thus restrained effectively the second pyrolysis of oil gas, and then improve the yield of pyrolytic tar, and pyrolysis gas is not diluted by gaseous heat-carrier, pyrolysis gas calorific value is high, good in economic efficiency, heat accumulation type radiant tube is coordinated additionally by arranging whipping appts in reactor, agitator arm is in the process carrying out back rotation, stacking material is loosened, increase the voidage between stacking material, reduce pyrolytic tar gas through material bed pressure drop, make the pyrolytic tar gas produced can pass rapidly through material bed arrival oil gas delivery line, the pyrolytic tar gas produced can be derived by oil gas delivery line in time, and the coking of radiator tube upper end can be avoided, thus avoid affecting heat transfer efficiency.
According to embodiments of the invention, with reference to figure 3, moving bed pyrolysis reactor comprises further: hopper 19, screw feeder 20 and spiral discharging machine 21.
According to volume embodiment of the present invention, hopper 19 is suitable for storage and treats pyrolysis material.
According to embodiments of the invention, screw feeder 20 is connected with material inlet 101 with hopper 19 respectively, and is suitable for treat that pyrolysis material is supplied in reactor through material inlet in hopper.
According to embodiments of the invention, spiral discharging machine 21 is arranged on the below of reactor, and exports 102 with semicoke and be connected.
Particularly, regulated by the variable valve on adjustment gas pipeline and pass into the accurate temperature controlling of the realizations such as the flow of the combustion gas of unidirectional heat accumulation type radiant tube to pyrolytic process, reactor upper temp scope is made to be 680 ~ 730 DEG C, the flow being passed into the combustion gas of heat accumulation type radiant tube by adjustment makes reactor middle portion temperature scope be 500 ~ 650 DEG C, the flow being passed into the combustion gas of heat accumulation type radiant tube by adjustment makes reactor lower part temperature range be 500 ~ 600 DEG C, material enters reactor in through screw feeder from material inlet from hopper, material scatter after the drying of reactor top, material is evenly scattered in the middle part of reactor pyrolytic reaction occurs, and the whipping appts in reactor can make agitator arm in the process carrying out back rotation, stacking material is loosened, increase the voidage between stacking material, reduce pyrolytic tar gas through material bed pressure drop, the pyrolytic tar gas produced can be passed rapidly through, and material bed arrival oil gas delivery line enters, the pyrolytic tar gas generated exports in gas gathering manifold through gas-collecting branch pipe, and the semicoke that pyrolysis produces drains into spiral discharging machine from semicoke outlet.
As mentioned above, can have according to the moving bed pyrolysis reactor of the embodiment of the present invention and be selected from following advantage one of at least:
Moving bed pyrolysis reactor according to the embodiment of the present invention adopts heat accumulation type radiant tube heat supply, and reactive system structure is simple, easy to operate, internal temperature field uniform, controllable;
1 ~ 2 oil gas delivery line is provided with according to bottom the every root heat accumulation type radiant tube of the moving bed pyrolysis reactor of the embodiment of the present invention, for deriving pyrolytic tar gas fast, restrained effectively the second pyrolysis of pyrolytic tar, pyrolytic tar quality better, productive rate is high, meanwhile, pyrolysis coal gas is not diluted by carrier gas, and calorific value is high;
Controlled according to the moving bed pyrolysis temperature of reactor field of the embodiment of the present invention, can be different according to different material pyrolysis characteristics, reasonably regulating and controlling temperature field and temperature field length.
Below with reference to specific embodiment, present invention is described, it should be noted that, these embodiments are only descriptive, and do not limit the present invention in any way.
Embodiment 1
The present embodiment 1 utilizes the moving bed pyrolysis reactor of Fig. 1-3 to process brown coal.The technical analysis of brown coal: Mad%:6.75%, Vad%:31.59%, Aad%:5.41%, Fcad%:56.25%.
Processing parameter: heat accumulation type radiant tube reactor drying and dehydrating district temperature is 690 DEG C, and pyrolysis reaction region temperature is 625 DEG C, and semicoke maturation zone temperature is 594 DEG C, heat accumulation type radiant tube reactor internal pressure 2.51Kpa.Pyrolysis tertiary industry distributes: pyrolytic tar 17.4%, pyrolysis gas 12.8%, semicoke 69.8%.
Embodiment 2
The present embodiment 2 utilizes the moving bed pyrolysis reactor of Fig. 1-3 to process rice husk.The technical analysis of rice husk: Mad%:6.56%, Vad%:65.17%, Aad%:11.52%, Fcad%:16.75%.Ultimate analysis: Cad%:40.69%, Had%:4.96%, Nad%:0.05%, Oad%; 35.13%.
Processing parameter: heat accumulation type radiant tube reactor drying and dehydrating district temperature is 680 DEG C, and pyrolysis reaction region temperature is 560 DEG C, and semicoke maturation zone temperature is 520 DEG C, heat accumulation type radiant tube reactor internal pressure 4.77Kpa.Pyrolysis tertiary industry distributes: pyrolytic tar 43.3%, pyrolysis gas 17.1%, semicoke 39.6%.
In the description of this specification sheets, specific features, structure, material or feature that the description of reference term " embodiment ", " some embodiments ", " example ", " concrete example " or " some examples " etc. means to describe in conjunction with this embodiment or example are contained at least one embodiment of the present invention or example.In this manual, to the schematic representation of above-mentioned term not must for be identical embodiment or example.And the specific features of description, structure, material or feature can combine in one or more embodiment in office or example in an appropriate manner.In addition, when not conflicting, the feature of the different embodiment described in this specification sheets or example and different embodiment or example can carry out combining and combining by those skilled in the art.
Although illustrate and describe embodiments of the invention above, be understandable that, above-described embodiment is exemplary, can not be interpreted as limitation of the present invention, and those of ordinary skill in the art can change above-described embodiment within the scope of the invention, revises, replace and modification.
Claims (10)
1. a moving bed pyrolysis reactor, is characterized in that, comprising:
Material inlet and semicoke outlet;
Described material inlet is positioned at the top of described reactor;
Described semicoke outlet is positioned at the bottom of described reactor;
Heat accumulation type radiant tube, the short transverse multilayer of described heat accumulation type radiant tube in the inside of described moving bed pyrolysis reactor along described reactor is arranged, every layer has many heat accumulation type radiant tubes parallel to each other in the horizontal direction;
Oil gas derives pipeline, and the tube wall of described oil gas derivation pipeline is provided with through hole;
Whipping appts, described whipping appts comprises stir shaft and is connected to the multiple agitator arms on described stir shaft, and described stir shaft is extend into the inside of described reactor by described semicoke outlet and is configured to rotate in described reactor;
Effuser, the gas-collecting branch pipe that described effuser comprises gas gathering manifold and is connected with described gas gathering manifold,
Wherein, it is outside that described gas gathering manifold is arranged on described reactor vertically,
The sidewall that described gas-collecting branch pipe extends through described reactor to extend in described reactor and derives pipeline with described oil gas and is connected.
2. reactor according to claim 1, is characterized in that, described gas-collecting branch pipe is multiple, and arranged parallel to each other along the length direction of described gas gathering manifold,
Optional, described gas-collecting branch pipe is perpendicular to described gas collecting main pipe.
3. reactor according to claim 1, is characterized in that, described oil gas is derived pipeline and arranged along the short transverse multilayer of described reactor, and every layer has many oil gas derivation pipelines parallel to each other in the horizontal direction,
Optional, described oil gas derives pipeline and described heat accumulation type radiant tube is arranged in parallel, and the described heat accumulation type radiant tube left and right sides is separately symmetrically arranged with two oil gas derivation pipelines.
4. reactor according to claim 3, is characterized in that, it is that described oil gas derives the 1/2-3 of pipe diameter d doubly that described oil gas derives pipeline with the spacing of the tube wall of contiguous described heat accumulation type radiant tube.
5. the reactor according to any one of claim 1-4, is characterized in that, the tube wall of described oil gas derivation pipeline is provided with multiple through hole, and preferably, described through hole is derived on the length direction of pipeline at described oil gas and is uniformly distributed.
6. reactor according to claim 5, is characterized in that, oil gas described in same layer is derived pipeline and is communicated to same described gas-collecting branch pipe.
7. the reactor according to any one of claim 1-6, is characterized in that, described agitator arm is between heat accumulation type radiant tube layer and oil gas delivery line channel layer.
8. the reactor according to any one of claim 1-7, is characterized in that, described agitator arm is perpendicular to described stir shaft, and spaced apart along the length direction of described stir shaft.
9. reactor according to claim 8, is characterized in that, the adjacent projections of described agitator arm on the same cross section of described stir shaft at an angle.
10. the reactor according to any one of claim 1-9, is characterized in that, the angle ranging from 0 ~ 90 degree, not containing end value, preferably, the angle ranging from 30 ~ 90 degree, not containing 90 degree.
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